CN113023886A - Fluidized bed-microaerobic multistage AO denitrification sewage treatment device and treatment process - Google Patents
Fluidized bed-microaerobic multistage AO denitrification sewage treatment device and treatment process Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 68
- 230000008569 process Effects 0.000 title claims abstract description 61
- 239000010865 sewage Substances 0.000 title claims abstract description 37
- 238000005273 aeration Methods 0.000 claims abstract description 124
- 239000010802 sludge Substances 0.000 claims abstract description 113
- 238000010992 reflux Methods 0.000 claims abstract description 98
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 94
- 230000008929 regeneration Effects 0.000 claims abstract description 50
- 238000011069 regeneration method Methods 0.000 claims abstract description 50
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 238000004062 sedimentation Methods 0.000 claims abstract description 23
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 34
- 229910052760 oxygen Inorganic materials 0.000 claims description 34
- 239000001301 oxygen Substances 0.000 claims description 34
- 238000005276 aerator Methods 0.000 claims description 33
- 239000000945 filler Substances 0.000 claims description 10
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 238000004065 wastewater treatment Methods 0.000 claims 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 20
- 229910052799 carbon Inorganic materials 0.000 abstract description 20
- 230000008901 benefit Effects 0.000 abstract description 8
- 238000004134 energy conservation Methods 0.000 abstract description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 33
- 229910052757 nitrogen Inorganic materials 0.000 description 17
- 230000001276 controlling effect Effects 0.000 description 12
- 230000000694 effects Effects 0.000 description 10
- 241000894006 Bacteria Species 0.000 description 8
- 230000001376 precipitating effect Effects 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000013461 design Methods 0.000 description 5
- 229910052698 phosphorus Inorganic materials 0.000 description 5
- 239000011574 phosphorus Substances 0.000 description 5
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 244000005700 microbiome Species 0.000 description 4
- 206010021143 Hypoxia Diseases 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 230000001546 nitrifying effect Effects 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- IPRNXEUYCDWBTL-UHFFFAOYSA-N ON=O.ON=O.ON=O.N.N Chemical compound ON=O.ON=O.ON=O.N.N IPRNXEUYCDWBTL-UHFFFAOYSA-N 0.000 description 2
- VCHHVWAFYWAVIX-UHFFFAOYSA-L [O-]N=O.[O-]N=O.[O-][N+]([O-])=O.N.[NH6+3] Chemical compound [O-]N=O.[O-]N=O.[O-][N+]([O-])=O.N.[NH6+3] VCHHVWAFYWAVIX-UHFFFAOYSA-L 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000593 degrading effect Effects 0.000 description 2
- 230000001079 digestive effect Effects 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 241001453382 Nitrosomonadales Species 0.000 description 1
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- Environmental & Geological Engineering (AREA)
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Abstract
The invention discloses a fluidized bed-microaerobic multistage AO denitrification sewage treatment device and a treatment process, wherein the device comprises a fluidized bed anaerobic zone, a fluidized bed anoxic zone I, an aeration zone I, a fluidized bed anoxic zone II, an aeration zone II, a maneuvering zone, an aerobic zone and a secondary sedimentation tank which are arranged along the water flow direction; a sludge regeneration zone is arranged at the front end of the fluidized bed anoxic zone I, and gates are arranged from the anaerobic zone of the fluidized bed to the sludge regeneration zone and the fluidized bed anoxic zone I; the device is also provided with a multi-point water inlet system, a multi-section mixed liquid internal reflux system, a sludge external reflux system and a precise aeration system; different sewage treatment processes can be realized through the device, the device is suitable for various water inlet quality and water outlet requirements, and has the advantages of land conservation, high efficiency, low carbon, energy conservation and the like.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a fluidized bed-microaerobic multistage AO denitrification sewage treatment device and a treatment process.
Background
At present, the sewage discharge amount is increased year by year in the sewage treatment industry, the pollution load exceeds the water environment capacity, and the water eutrophication is tighterSerious problems and the like. With the increasing of the sewage discharge standard, the existing traditional sewage treatment process comprises A2The method comprises the following steps of/O, MUCT, oxidation ditch, SBR and the like, and has the problems of low total nitrogen and total phosphorus removal efficiency, low effluent water discharge standard, high energy consumption and the like.
In order to fully utilize the denitrification capability of a limited carbon source strengthening treatment facility in sewage and improve the treatment capability and standard, a multi-section multi-mode A/O high-efficiency denitrification process and a micro-aerobic (aeration and anoxic) multi-stage AO high-efficiency strengthening denitrification process have been successively proposed, the denitrification efficiency is greatly improved compared with that of the traditional process, the energy consumption is also greatly reduced, and good environmental benefit and economic benefit are obtained. But still has the problems of high cost, large energy consumption, large occupied area and the like.
Disclosure of Invention
In view of the above, the invention provides a fluidized bed-microaerobic multistage AO enhanced denitrification sewage treatment device, which has the advantages of land saving, high efficiency, low carbon, energy saving and the like, can adjust the operation mode according to the water quality condition of inlet water, and has strong applicability.
In order to achieve the above purpose, the technical scheme of the invention is as follows:
a fluidized bed-microaerobic multistage AO denitrification sewage treatment plant comprises a fluidized bed anaerobic zone, a fluidized bed anoxic zone I, an aeration zone I, a fluidized bed anoxic zone II, an aeration zone II, a maneuvering zone and an aerobic zone which are arranged along the water flow direction, wherein the effluent of the aerobic zone enters a secondary sedimentation tank; a sludge regeneration zone is arranged at the front end of the anoxic zone I of the fluidized bed, a first gate is arranged between the anaerobic zone of the fluidized bed and the sludge regeneration zone, and a second gate is arranged between the anaerobic zone of the fluidized bed and the anoxic zone I of the fluidized bed;
biological fillers are added into the tanks of the anaerobic zone of the fluidized bed, the anoxic zone I of the fluidized bed and the anoxic zone II of the fluidized bed; plug flow devices are arranged in the anaerobic zone of the fluidized bed, the anoxic zone I of the fluidized bed, the anoxic zone II of the fluidized bed and the maneuvering zone;
the device is also provided with a multi-point water inlet system, a multi-section mixed liquid internal reflux system, a sludge external reflux system and a precise aeration system;
the multi-point water inlet system is internally provided with 4 water inlet pipe orifices, each water inlet pipe orifice is provided with a flow regulating valve, and the water inlet pipe orifices are respectively positioned in an anaerobic zone of the fluidized bed, an anoxic zone I of the fluidized bed, an anoxic zone II of the fluidized bed and a maneuvering zone;
the multi-section mixed liquid reflux system comprises mixed liquid reflux inlets arranged in an anoxic zone I of the fluidized bed, an anoxic zone I of the fluidized bed and a maneuvering zone and mixed liquid reflux outlets arranged in an aeration zone I, an aeration zone II and an aerobic zone;
the sludge in the sludge external reflux system flows back to the anaerobic zone and the sludge regeneration zone of the fluidized bed from the secondary sedimentation tank through a pipeline;
the precise aeration system comprises aerators arranged at the bottoms of a sludge regeneration area, an aeration I area, an aeration II area, a maneuvering area and an aerobic area, and the aerator of each area is provided with an independent aeration pipe and a flow control valve.
Preferably, the water inflow of the water inlet pipe orifices of the anaerobic zone, the anoxic zone I of the fluidized bed, the anoxic zone II of the fluidized bed and the maneuvering zone is 0-50% of Q, 0-30% of Q and 0-30% of Q respectively; the backflow amount of the sludge external backflow system is 50-100% Q.
It can be understood that the device such as a control valve and a reflux pump is also arranged in the sludge external reflux system and the multi-section mixed liquid internal reflux system, the accurate aeration system also comprises a blower room and the like which are necessary, the prior art is adopted, and the detailed description is omitted.
The invention also provides a sewage treatment process using the fluidized bed-microaerobic multistage AO denitrification sewage treatment device, wherein a precise aeration system, a multi-section mixed liquid internal reflux system, a multi-point water inlet system and the like in the device are arranged according to the specific conditions of the water quality of inlet water to obtain different treatment process modes, and the specific treatment process modes comprise the following steps:
(1) fluidized bed-two stage AO process mode:
closing the water inlet pipe orifices of the maneuvering area, and opening the other 3 water inlet pipe orifices; opening the first gate and closing the second gate; closing a flow pusher in the maneuvering zone, opening aerators at the bottom of the aeration zone I, the aeration zone II and the maneuvering zone, and controlling aeration quantity to adjust all the three zones into aerobic zones; closing the mixed liquid internal reflux outlet of the aeration II area and the mixed liquid internal reflux inlet of the maneuvering area, and reserving the reflux from the aerobic area to the fluidized bed anoxic II area and the reflux from the aeration I area to the fluidized bed anoxic I area; opening the secondary sedimentation tank until the sludge in the sludge regeneration zone and the anaerobic zone of the fluidized bed flows back outside; thereby forming a combined two-stage AO process of anaerobic zone-anoxic zone-aerobic zone.
(2) Fluidized bed-three stage AO process mode:
opening the 4 water inlet pipe orifices, opening the first gate and closing the second gate; turning off an aerator in the maneuvering zone, and turning on a flow pusher in the maneuvering zone to adjust the maneuvering zone into an anoxic zone; controlling the aeration rate in the aeration I area and the aeration II area to adjust the aeration rate into an aerobic area; opening the aerobic zone to flow back to the mobile zone, aerating the aerobic zone to flow back to the anoxic zone II of the fluidized bed, and aerating the aerobic zone to flow back to the anoxic zone I of the fluidized bed; opening the secondary sedimentation tank to the sludge regeneration zone and the sludge reflux of the anaerobic zone of the fluidized bed; form a three-stage AO process of the combination of anaerobic zone-anoxic zone-aerobic zone.
(3) Fluidized bed-microaerobic two-stage AO process mode:
closing the water inlet pipe orifice of the maneuvering area, opening other water inlet pipe orifices, closing the first gate, and opening the second gate; starting an aerator in the sludge regeneration area, and carrying out controlled aeration; closing a flow pushing device in the maneuvering zone, controlling the aeration rate of an aerator in the aeration I zone, the aeration II zone and the maneuvering zone, and adjusting the 3 zones into micro aerobic zones; closing an internal reflux outlet of the aeration II area and an internal reflux inlet of the maneuvering area, and keeping the reflux from the aerobic area to the anoxic II area of the fluidized bed and the reflux from the aeration I area to the anoxic I area of the fluidized bed; opening the secondary sedimentation tank to the sludge regeneration zone and the sludge reflux of the anaerobic zone of the fluidized bed; thereby forming a combined fluidized bed-micro aerobic secondary AO process of (an anaerobic zone + a sludge regeneration zone) -an anoxic zone-a micro aerobic zone-an anoxic zone-a micro aerobic or aerobic zone'.
(4) Fluidized bed-microaerobic three-stage AO process mode:
opening the four water inlet pipe orifices, closing the first gate and opening the second gate; starting aeration at the bottom of the sludge regeneration area, and carrying out controlled aeration; starting an aerator in the sludge regeneration area, and carrying out controlled aeration; opening aerators in the aeration I area and the aeration II area, controlling aeration amount, and adjusting the 2 areas into micro aerobic areas; closing an aerator in the maneuvering zone, opening a flow pusher in the maneuvering zone, and adjusting the maneuvering zone into an anoxic zone; opening the aerobic zone to flow back to the mobile zone, aerating the aerobic zone to flow back to the anoxic zone II of the fluidized bed, and aerating the aerobic zone to flow back to the anoxic zone I of the fluidized bed; opening the secondary sedimentation tank to the sludge regeneration zone and the sludge reflux of the anaerobic zone of the fluidized bed; thereby forming a combined fluidized bed-microaerobic three-stage AO process of (an anaerobic zone + a sludge regeneration zone) -an anoxic zone-a microaerobic zone-an anoxic zone-an aerobic zone).
Preferably, the dissolved oxygen value of the anaerobic zone of the fluidized bed is 0-0.2 mg/L, the dissolved oxygen value of the anoxic zone is 0.2-0.5mg/L, and the dissolved oxygen value of the aerobic zone is 2mg/L or more. The anoxic zone comprises the anoxic zones of the two original fluidized beds and also comprises anoxic zones adjusted by maneuvering zones in different modes; the aerobic zone not only comprises an aerobic zone, but also comprises an aerobic zone adjusted by an aeration zone and a maneuvering zone in different modes.
Preferably, the dissolved oxygen value of the micro-aerobic area is 0.2-1.0 mg/L, and the dissolved oxygen value of the sludge regeneration area is 0.2-0.5 mg/L.
It should be noted that:
micro-aerobic is also called aeration anoxic, the concept breaks through the concept that the traditional treatment process can only carry out nitration reaction well under the environment of high dissolved oxygen, and a large amount of ammonia nitrogen in an aeration anoxic zone occupying a larger proportion of the tank volume is nitrated at a higher reaction rate, thereby realizing the short-range denitrification of 'ammonia-nitrite-nitrogen'. The short-range reaction not only improves the denitrification efficiency, but also reduces the carbon requirement of denitrification, reduces the C/N requirement level of the system and can obviously improve the removal rate of total nitrogen.
The fluidized bed biological filler can provide a carrier for biological bacteria, overcomes the defects of low mass transfer efficiency, poor treatment efficiency, high fluidization power and the like, fully utilizes the advantages of an activated sludge method by applying the basic principle of a biomembrane method, and realizes the activated sludge mode operation of a biomembrane process. The method is beneficial to realizing anaerobic ammonia oxidation, and the removal rate of the anaerobic ammonia nitrogen and the removal load of the nitrogen are high, so that the occupied area of the process can be reduced, and the capital construction cost of the process can be reduced; the anaerobic ammonia oxidizing bacteria grow slowly, the yield is low, the amount of excess sludge is small, the sludge disposal cost is low, and the purposes of high efficiency and energy conservation are really achieved.
The invention has the beneficial effects that:
1) the process operation modes can be adjusted to be a fluidized bed two-stage AO process, a fluidized bed three-stage AO process, a fluidized bed-microaerobic two-stage AO process, a fluidized bed-microaerobic three-stage AO process and the like according to different inlet water quality conditions and outlet water requirements;
2) the sewage treatment effect is good, particularly the total nitrogen treatment effect is good, the effective carbon source in the inlet water can be utilized to the maximum extent, and the operation cost is low;
3) the design concept of micro-aerobic (aeration and oxygen deficiency) is introduced into the fluidized bed-micro-aerobic two-stage AO process and the fluidized bed-micro-aerobic three-stage AO process. Not only can realize simultaneous nitrification and denitrification of 5-step denitrification of ammonia-nitrite-nitrate-nitrite-nitrogen gas, but also can realize 3-step short-range denitrification of ammonia-nitrite-nitrogen gas;
4) the anaerobic area and part of the anoxic area are added with fluidized bed biological fillers, so that the defects of low mass transfer efficiency, poor treatment efficiency, high fluidization power and the like of the anaerobic area and part of the anoxic area are overcome, the basic principle of a biomembrane method is applied, the advantages of an activated sludge method are fully utilized, and the activated sludge mode operation of a biomembrane process is realized;
5) the fluidized bed-microaerobic secondary AO process and the fluidized bed-microaerobic tertiary AO process are provided with sludge regeneration zones, and the increased storage capacity of nitrifying bacteria enables a biochemical system to maintain the proportion of healthy autotrophic nitrifying bacteria, improves the activity of the nitrifying bacteria and other bacteria and improves the reaction efficiency of the system, thereby achieving the purpose of prolonging the sludge age and improving the treatment efficiency;
6) the multipoint water inflow reasonably distributes the carbon source of the inflow water, firstly, the carbon source requirement of biological denitrification is ensured, the biological phosphorus removal can be ensured on the premise of meeting the denitrification, and the stable and standard discharge of the effluent quality of the whole system is ensured;
7) each aerobic section of the biochemical pool is provided with an independent pipeline for air supply, and is provided with a streamline control valve, a thermal flowmeter and an accurate aeration system control system; the effect is good, the oxygen utilization rate is high, and the energy-saving effect is good;
8) because fluidized bed biological fillers are added in the anaerobic tank and the anoxic tank, the design concept of microaerobic and sludge regeneration is introduced, compared with the traditional process (such as improved AAO and multi-stage AO process), the process saves land by 10-30%, reduces aeration energy consumption by 30-50%, and improves decarburization efficiency by 20-30%.
Drawings
FIG. 1 is a schematic view of a sewage treatment apparatus according to embodiment 1;
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail with reference to the accompanying drawings and specific embodiments. The specific embodiments described herein are merely illustrative of the invention and are not intended to be limiting.
Example 1
As shown in fig. 1, a fluidized bed-microaerobic multistage AO denitrification sewage treatment device comprises a fluidized bed anaerobic zone 1, a fluidized bed anoxic zone i 3, an aeration zone i 4, a fluidized bed anoxic zone ii 5, an aeration zone ii 6, a maneuvering zone 7 and an aerobic zone 8 which are sequentially arranged along the water flow direction, wherein the effluent at the tail end of the aerobic zone 8 enters a sedimentation tank 9 for sludge sedimentation; the front end in I district 3 of fluidized bed oxygen deficiency still is equipped with sludge regeneration district 2, is provided with first gate 10 between fluidized bed anaerobic zone 1 and the sludge regeneration district 2, is provided with second gate 11 between fluidized bed anaerobic zone 1 and I district 3 of fluidized bed oxygen deficiency, and first gate 10 and second gate 11 are used for controlling the flow direction of sewage in the fluidized bed anaerobic zone 1.
The device is also provided with a multi-point water inlet system 14, a multi-section mixed liquid internal reflux system 15, a sludge external reflux system 16 and a precise aeration system 17.
The following description will be made separately for each processing region:
the anaerobic zone 1 of the fluidized bed is provided with a water inlet pipe orifice, a flow regulating valve is arranged at the pipe orifice, biological fillers 12 are added into the tank, and sludge external reflux is also arranged. An anaerobic environment is created in the area, and anaerobic microorganism growth is facilitated; the phosphorus-accumulating bacteria can release phosphate radicals under the condition that the activated sludge adsorbs and degrades organic matters. In order to remove the influence of nitrate nitrogen brought by the returned sludge on the dephosphorization effect, an anaerobic zone is arranged in front of the anoxic zone and is used for removing nitrate in the returned sludge, the sludge sedimentation performance is improved, and the dissolved oxygen value is controlled to be 0-0.2 mg/l. The water inlet pipe orifice is matched with the sludge backflow point, so that the nitrogen and phosphorus removal effect can be effectively improved. The water inflow of the water inlet pipe is 0-50% Q, the water inflow of the water inlet pipe is adjusted according to the water quality of inlet water and the standard requirement of outlet water, and a part of inlet water directly enters the anaerobic zone to release phosphorus in the anaerobic state of sludge. The region is provided with the impeller, so that the stirring uniformity of the anaerobic zone is ensured, the flow velocity is not less than 0.3m/s, the effluent can enter the sludge regeneration zone or the anoxic zone, the effluent can be flexibly adjusted through the gates, and the retention time of the anaerobic zone is about 1.0-1.5 h.
The sludge regeneration zone 2 is arranged to prolong the sludge age on the premise of not improving the concentration of the mixed liquid entering the secondary sedimentation tank, maximize the number of microorganisms in the biological treatment system, realize reliable nitrification and further ensure the quality of the effluent. An aerator is arranged at the bottom of the area, the returned sludge of the secondary sedimentation tank 9 returns to a sludge regeneration area, controlled aeration is carried out in the regeneration tank, the dissolved oxygen value is controlled to be 0.2-0.5mg/l so as to maintain the microbial activity, and then the returned sludge returns to the anoxic tank.
The first anoxic zone 3 and the second anoxic zone 5 of the fluidized bed are both provided with water inlet pipe orifices, flow regulating valves are arranged at the pipe orifices, a mixed liquid internal reflux inlet is arranged, and biological fillers 12 are added in the tank. The anoxic pond creates an anoxic environment, which is beneficial to the growth of anoxic microorganisms; the activated sludge nitrogen release agent is used for adsorbing and degrading organic matters by activated sludge, and can also be used for generating nitrogen and releasing nitrate nitrogen in the backflow mixed liquor under the action of denitrifying bacteria. The region is provided with a flow impeller to ensure that the anoxic region is stirred uniformly and the flow velocity is not less than 0.3 m/s.
Aerators are arranged at the bottom of the aeration I area 4 and the aeration II area 6, and the areas can be adjusted into aerobic areas or micro-aerobic areas (limited anoxic aeration) by accurately controlling aeration rate. The oxygen demand is greatly reduced and the oxygen transfer efficiency is greatly improved by micro-aerobic design. In the reaction front section, the limited anoxic aeration is carried out on the reaction front section, so that the area has strains such as oxygen, carbon source organic matters, ammonia, nitrification/denitrification and the like, and is in an anoxic state in a macroscopic view, and the method can be realized under the environment that: ammonia-nitrite-nitrate-nitrite-nitrogen, simultaneous nitrification and denitrification with 5-step denitrification, can also occur: ammonia-nitrite-nitrogen, 3-step short-cut denitrification.
The bottom of the maneuvering zone 7 is provided with an aerator, the inside of the maneuvering zone is provided with a submersible flow device 13, a water inlet pipe orifice and a mixed liquid internal reflux inlet, and the maneuvering zone can be flexibly adjusted into an aerobic zone, a micro-aerobic zone or an anoxic zone by opening and closing the aerator, the submersible flow device, a sewage inlet and a digestive juice inlet according to actual requirements. For example: if the C/N ratio of inlet water is higher, closing the inlet valve, and no additional carbon source is needed, then the area is an aerobic area (the DO value is controlled at 2mg/l) or a micro-aerobic area (the DO value is controlled at 0.5-1.0 mg/l); if the C/N ratio of inlet water is lower, opening a water inlet valve, and allowing part of sewage to enter the zone to make up carbon source required by denitrification, wherein the zone is a third anoxic zone (DO value is controlled to be 0.2-0.5 mg/l); meanwhile, in order to utilize the carbon source to the maximum extent to complete denitrification, the air supply valve is closed in the area, and the impeller is opened to complete the stirring function.
An aerator is arranged in the bottom of the aerobic zone 8 and is used for creating an aerobic environment, which is beneficial to the growth of aerobic microorganisms. It has the functions of adsorbing and degrading organic matter with well-maintained active sludge and oxidizing carbon element in the organic matter into CO2And H2O; the nitrogen element is oxidized into nitrite nitrogen and nitrate nitrogen. The DO value of the aerobic zone is controlled to be 2mg/L or more, preferably 2mg/L to 3 mg/L.
The multi-point water inlet system 14 can reasonably distribute water inlet carbon sources, firstly, the carbon source requirement of biological denitrification is ensured, the carbon source adding is reduced to the maximum extent, the operation cost is saved, the biological phosphorus removal can be ensured on the premise of meeting the denitrification, and the stable and standard discharge of the water quality of the outlet water of the whole system is ensured.
The multi-stage mixed liquor internal reflux system 15 is used for refluxing the digestive juice containing a large amount of nitrate nitrogen from the aerobic area to the anoxic area for denitrification in the anoxic area.
The accurate aeration system 17 comprises aerators arranged in each area, and the aerators are connected with independent gas supply pipelines which are provided with flow meters and control valves. Can provide the demand tolerance that corresponds the region according to actual demand, the accurate not only can practice thrift the air-blower power consumption, can also stabilize the dissolved oxygen concentration of each processing region, improves the treatment effect.
And the sludge external reflux system 16 is used for refluxing the sludge in the secondary sedimentation tank 9 to the sludge regeneration zone 2 and the fluidized bed anaerobic zone 1, wherein the sludge reflux amount is 50-100% Q.
Example 2
Fluidized bed-two stage AO process, using the apparatus of example 1, operating scheme as follows:
closing the water inlet pipe orifices of the maneuvering area 7, and opening the other 3 water inlet pipe orifices; opening the first shutter 10 and closing the second shutter 11; closing a flow pushing device 13 in the maneuvering zone 7, opening aerators at the bottoms of the aeration zone I4, the aeration zone II 6 and the maneuvering zone 7, controlling aeration quantity to adjust all the three zones into aerobic zones, and opening the aerators in the aerobic zones; closing the mixed liquid internal reflux outlet of the aeration II area 6, closing the mixed liquid internal reflux inlet of the maneuvering area 7, and keeping the reflux from the aerobic area 8 to the fluidized bed anoxic II area 5 and the reflux from the aeration I area 4 to the fluidized bed anoxic I area 3; opening the secondary sedimentation tank 9 to return sludge in the sludge regeneration zone 2 and the fluidized bed anaerobic zone 1; thereby forming a standard combined two-stage AO process of anaerobic zone-anoxic zone-aerobic zone.
Then sewage is introduced and treated in each treatment area. Wherein the operating parameters of each zone are as follows:
the water inflow of water inlet pipe orifices of an anaerobic zone 1, an anoxic zone I3 and an anoxic zone II 5 of the fluidized bed is respectively 0-50% Q, 0-50% Q and 0-30% Q;
secondly, opening a flow pushing device 13 in the anaerobic zone 1 of the fluidized bed to ensure that the water flow speed in the zone is not less than 0.3m/s so as to prevent sludge from precipitating and simultaneously keeping the dissolved oxygen value in the zone to be 0-0.2 mg/L;
thirdly, starting a flow impeller in an anoxic I area 3 and an anoxic II area 5 of the fluidized bed to ensure that the water flow speed of an anoxic area is not less than 0.3m/s so as to prevent sludge from precipitating, and simultaneously keeping the dissolved oxygen value in the tank to be 0.2-0.5 mg/L;
fourthly, keeping the dissolved oxygen amount in the aeration I area 4, the maneuvering area 7, the aeration II area 6 and the aerobic area 8 to be 2mg/L or more;
the internal reflux is divided into two stages of reflux: refluxing from the aerobic zone 8 to an anoxic zone II 5 of the fluidized bed, wherein the reflux amount is 100-200% Q; refluxing from the aeration I area 4 to the fluidized bed anoxic I area 3, wherein the reflux amount is 50-100% Q;
and sixthly, externally refluxing the sludge to flow back to the fluidized bed anaerobic zone 1 and the sludge regeneration zone 2 from the secondary sedimentation tank 9, wherein the reflux amount is 50-100% Q, and the sludge concentration in the fluidized bed anaerobic zone 1, the fluidized bed anoxic zone I3, the fluidized bed anoxic zone II 5 and the aerobic zone 8 is 5000-3500 mg/L.
This mode applies to the following cases: the carbon source of inlet water is sufficient, and the total nitrogen standard of outlet water is high (the total nitrogen requirement is less than 15 mg/L); or the carbon source of inlet water is poor, and the standard of total nitrogen of outlet water is high (first-grade A standard, total nitrogen is 15mg/L)
Example 3
Fluidized bed-two stage AO process, using the apparatus of example 1, operating scheme as follows:
opening the 4 water inlet pipe orifices, opening the first gate 10 and closing the second gate 11; turning off an aerator in the maneuvering zone 7, and turning on a flow pusher in the maneuvering zone 7 to adjust the maneuvering zone 7 to an anoxic zone; controlling the aeration rate in the aeration I area 4 and the aeration II area 6 to adjust the aeration rate into an aerobic area; opening the reflux from the aerobic zone 8 to the mobile zone 7, the reflux from the aeration zone II 6 to the fluidized bed anoxic zone II 5, and the reflux from the aeration zone I4 to the fluidized bed anoxic zone I3; opening the secondary sedimentation tank 9 to return sludge in the sludge regeneration zone 2 and the fluidized bed anaerobic zone 1; thereby forming a three-stage AO process of combining an anaerobic zone, an anoxic zone, an aerobic zone, an anoxic zone and an aerobic zone.
Then sewage is introduced and treated in each treatment area. Wherein the operating parameters of each zone are as follows:
the water inflow of water inlet pipe orifices of an anaerobic zone 1, an anoxic zone I3, an anoxic zone II 5 and a maneuvering zone 7 of a fluidized bed is respectively 0-50% Q, 0-30% Q and 0-30% Q;
secondly, opening a flow pushing device 13 in the anaerobic zone 1 of the fluidized bed to ensure that the water flow speed in the zone is not less than 0.3m/s so as to prevent sludge from precipitating and simultaneously keeping the dissolved oxygen value in the zone to be 0-0.2 mg/L;
thirdly, starting a flow impeller in an anoxic I area 3 and an anoxic II area 5 of the fluidized bed to ensure that the water flow speed of an anoxic area (including a maneuvering area 7) is not less than 0.3m/s so as to prevent sludge from precipitating, and simultaneously keeping the dissolved oxygen value in the tank to be 0.2-0.5 mg/L;
starting aerators in the aeration I area 4, the aeration II area 6 and the aerobic area 8, and keeping the dissolved oxygen amount of the aerobic area at 2mg/L or above;
fifth, the internal reflux is divided into three stages of reflux: refluxing from the aerobic zone 8 to the maneuvering zone 7, wherein the reflux amount is 100-200% Q; refluxing from the aeration II area 6 to the fluidized bed anoxic II area 5, wherein the reflux amount is 50-100% Q; refluxing from the aeration I area 4 to the fluidized bed anoxic I area 3, wherein the reflux amount is 50-100% Q;
and sixthly, externally refluxing the sludge, namely refluxing the sludge from the secondary sedimentation tank 9 to the fluidized bed anaerobic zone 1 and the sludge regeneration zone 2, wherein the reflux amount is 50-100% Q, and the sludge concentration in the fluidized bed anaerobic zone 1, the fluidized bed anoxic zone I3, the fluidized bed anoxic zone II 5 and the aerobic zone 8 is 6000-3500 mg/L.
This mode uses the following: the effluent standard is high and is required to reach the standard of surface four (the total nitrogen requirement is less than 10 mg/L); or the carbon source of the inlet water is insufficient, and the carbon source needs to be added externally, and the carbon source adding can be reduced by adopting multi-point water inlet, so that the total nitrogen removal rate is improved.
Example 4
The fluidized bed-microaerobic secondary AO process, using the apparatus of example 1, was operated as follows:
closing the water inlet pipe orifice of the maneuvering zone 7 and opening other water inlet pipe orifices, closing the first gate 10 and opening the second gate 11; starting an aerator in the sludge regeneration zone 2, and carrying out controlled aeration; closing a flow pushing device 13 in the maneuvering zone 7, controlling the aeration rates of aerators in the aeration I zone 4, the aeration II zone 6 and the maneuvering zone 7, and adjusting the 3 zones into micro aerobic zones; closing an internal reflux outlet of the aeration II area 6 and an internal reflux inlet of the maneuvering area 7, and keeping the reflux from the aerobic area 8 to the anoxic II area 5 of the fluidized bed and the reflux from the aeration I area 4 to the anoxic I area 3 of the fluidized bed; opening the secondary sedimentation tank 9 to return sludge in the sludge regeneration zone 2 and the fluidized bed anaerobic zone 1; thereby forming a combined fluidized bed-micro aerobic secondary AO process of (an anaerobic zone + a sludge regeneration zone) -an anoxic zone-a micro aerobic zone-an anoxic zone-a micro aerobic or aerobic zone'.
Then sewage is introduced and treated in each treatment area. Wherein the operating parameters of each zone are as follows:
the water inflow of water inlet pipe orifices of an anaerobic zone 1, an anoxic zone I3 and an anoxic zone II 5 of the fluidized bed is respectively 0-50% Q, 0-50% Q and 0-30% Q;
secondly, opening a flow pushing device 13 in the anaerobic zone 1 of the fluidized bed to ensure that the water flow speed in the zone is not less than 0.3m/s so as to prevent sludge from precipitating and simultaneously keeping the dissolved oxygen value in the zone to be 0-0.2 mg/L;
thirdly, starting bottom aeration in the sludge regeneration area for controlled aeration, and controlling the dissolved oxygen value to be 0.2-0.5 mg/L; starting a flow impeller in an anoxic I area 3 and an anoxic II area 5 of the fluidized bed to ensure that the water flow speed of an anoxic area is not less than 0.3m/s so as to prevent sludge from precipitating, and simultaneously keeping the dissolved oxygen value in the tank to be 0.2-0.5 mg/L;
starting aerators in the aeration I area 4, the aeration II area 6 and the maneuvering area 7 to carry out controlled aeration on the areas, wherein the dissolved oxygen value is 0.2-1.0 mg/L
Opening an aerator in the aerobic zone 8, and keeping the dissolved oxygen amount of the aerobic zone at 2mg/L or above;
sixthly, internal reflux is divided into two stages of reflux: refluxing from the tail end of the aerobic zone 8 to an anoxic zone II 5 of the fluidized bed, wherein the refluxing quantity is 100-200% Q; refluxing from the aeration I area 4 to the fluidized bed anoxic I area 3, wherein the reflux amount is 50-100% Q;
and the external reflux of the sludge is from the secondary sedimentation tank 9 to the fluidized bed anaerobic zone 1 and the sludge regeneration zone 2, the reflux amount is 50-100% Q, and the sludge concentration in the fluidized bed anaerobic zone 1, the fluidized bed anoxic zone I3, the fluidized bed anoxic zone II 5 and the aerobic zone 8 is 5000-3500 mg/L.
The process mode is an energy-saving process, the process introduces the design concepts of a fluidized bed, aeration anoxic and sludge regeneration, biological fillers are added in an anaerobic zone and an anoxic zone, functions of a sludge regeneration tank, an aeration anoxic zone and the like are added, and the denitrification effect is improved; and the fluidized bed biological filler can provide a carrier for biological bacteria, so that anaerobic ammonia oxidation is realized, and the aims of high efficiency and energy conservation are fulfilled. The process has good application prospect in the construction and upgrading reconstruction projects of high-emission standard sewage plants.
Example 5
The fluidized bed-microaerobic three-stage AO process, using the apparatus of example 1, was operated as follows:
opening the four water inlet pipe orifices, closing the first gate 10 and opening the second gate 11; starting aeration at the bottom of the sludge regeneration zone 2 for controlled aeration; opening aerators in an aeration I area 4 and an aeration II area 6, controlling aeration amount, and adjusting the 2 areas into micro aerobic areas; closing an aerator in the maneuvering zone 7, opening a flow pusher in the maneuvering zone 7, and adjusting the maneuvering zone 7 into an anoxic zone; opening the reflux from the aerobic zone 8 to the mobile zone 7, the reflux from the aeration zone II 6 to the fluidized bed anoxic zone II 5, and the reflux from the aeration zone I4 to the fluidized bed anoxic zone I3; opening the secondary sedimentation tank 9 to return sludge in the sludge regeneration zone 2 and the fluidized bed anaerobic zone 1; thereby forming a standard combined fluidized bed-micro aerobic three-stage AO process of (an anaerobic zone and a sludge regeneration zone) -an anoxic zone-a micro aerobic zone-an anoxic zone-an aerobic zone).
Then sewage is introduced and treated in each treatment area. Wherein the operating parameters of each zone are as follows:
the water inflow of water inlet pipe orifices of an anaerobic zone 1, an anoxic zone I3 and an anoxic zone II 5 of a fluidized bed is respectively 0-50% Q, 0-30% Q and 0-30% Q;
secondly, opening a flow pushing device 13 in the anaerobic zone 1 of the fluidized bed to ensure that the water flow speed in the zone is not less than 0.3m/s so as to prevent sludge from precipitating and simultaneously keeping the dissolved oxygen value in the zone to be 0-0.2 mg/L;
thirdly, starting bottom aeration in the sludge regeneration area for controlled aeration, and controlling the dissolved oxygen value to be 0.2-0.5 mg/L;
fourthly, the anoxic zone I3, the anoxic zone II 5 and the maneuvering zone 7 of the fluidized bed are anoxic zones, a flow impeller is started to ensure that the water flow speed of the anoxic zone is not less than 0.3m/s so as to prevent sludge from precipitating, and meanwhile, the dissolved oxygen value in the tank is kept to be 0.2-0.5 mg/L;
fifthly, opening an aeration I area 4 and an aeration II area 6 as micro aerobic areas, opening an aerator, and carrying out controlled aeration on the micro aerobic areas, wherein the dissolved oxygen value is 0.2-1.0 mg/L
Sixthly, opening an aerator in the aerobic zone 8 and keeping the dissolved oxygen of the aerobic zone at 2mg/L or above;
the internal reflux is divided into three stages: refluxing from the aerobic zone 8 to the maneuvering zone 7, wherein the reflux amount is 100-200% Q; refluxing from the aeration II area 6 to the fluidized bed anoxic II area 5, wherein the reflux amount is 50-100% Q; refluxing from the aeration I area 4 to the fluidized bed anoxic I area 3, wherein the reflux amount is 50-100% Q;
and eighthly, the external reflux of the sludge is from the secondary sedimentation tank 9 to the fluidized bed anaerobic zone 1 and the sludge regeneration zone 2, the reflux amount is 50-100% Q, and the sludge concentration in the fluidized bed anaerobic zone 1, the fluidized bed anoxic zone I3, the fluidized bed anoxic zone II 5 and the aerobic zone 8 is 6000-3500 mg/L.
The process introduces the design concepts of a fluidized bed, microaerobic (aeration and anoxic) and sludge regeneration, biological fillers are added in the anaerobic zone and the anoxic zone, functions of a sludge regeneration tank, a microaerobic zone and the like are added, and the denitrification effect is effectively improved. The process has obvious advantages in the construction of sewage plants with high requirements on the total nitrogen (the total nitrogen requirement is not more than 8mg/L) of the effluent.
It is to be understood that no matter how much of this specification appears, such as in the prior art or common general knowledge. The present embodiments are illustrative only and not intended to limit the scope of the present invention, and modifications and equivalents thereof by those skilled in the art are considered to fall within the scope of the present invention as set forth in the claims.
Claims (9)
1. A fluidized bed-microaerobic multistage AO denitrification sewage treatment device is characterized by comprising a fluidized bed anaerobic zone (1), a fluidized bed anoxic zone I (3), an aeration zone I (4), a fluidized bed anoxic zone II (5), an aeration zone II (6), a maneuvering zone (7) and an aerobic zone (8) which are arranged along the water flow direction, wherein the effluent of the aerobic zone (8) enters a secondary sedimentation tank (9); a sludge regeneration zone (2) is arranged at the front end of the fluidized bed anoxic zone I (3), a first gate (10) is arranged between the fluidized bed anaerobic zone (1) and the sludge regeneration zone (2), and a second gate (11) is arranged between the fluidized bed anaerobic zone (1) and the fluidized bed anoxic zone I (3);
biological fillers (12) are added into the tanks of the fluidized bed anaerobic zone (1), the fluidized bed anoxic zone I (3) and the fluidized bed anoxic zone II (5); plug-flow devices (13) are arranged in the fluidized bed anaerobic zone (1), the fluidized bed anoxic zone I (3), the fluidized bed anoxic zone II (5) and the maneuvering zone (7);
the device is also provided with a multi-point water inlet system (14), a multi-section mixed liquid internal reflux system (15), a sludge external reflux system (16) and a precise aeration system (17);
the multi-point water inlet system (14) comprises 4 water inlet pipe orifices, each water inlet pipe orifice is provided with a flow regulating valve, and the water inlet pipe orifices are respectively positioned in the anaerobic zone (1) of the fluidized bed, the anoxic zone I (3) of the fluidized bed, the anoxic zone II (5) of the fluidized bed and the maneuvering zone (7);
the multi-section mixed liquid internal reflux system (15) comprises a mixed liquid reflux inlet arranged in the fluidized bed anoxic zone I (3), the fluidized bed anoxic zone I (5) and the maneuvering zone (7) and a mixed liquid reflux outlet arranged in the aeration zone I (4), the aeration zone II (6) and the aerobic zone (8);
in the sludge external reflux system (16), sludge flows back to the fluidized bed anaerobic zone (1) and the sludge regeneration zone (2) from the secondary sedimentation tank (9) through pipelines;
the accurate aeration system (17) comprises aerators arranged at the bottoms of a sludge regeneration zone (2), an aeration I zone (4), an aeration II zone (6), a maneuvering zone (7) and an aerobic zone (8), and each aerator is provided with an independent aeration pipe and a flow control valve.
2. The fluidized bed-microaerobic multistage AO denitrogenation sewage treatment apparatus according to claim 1, wherein the water inflow of the water inlet pipe openings of the fluidized bed anaerobic zone (1), the fluidized bed anoxic I zone (3), the fluidized bed anoxic II zone (5) and the maneuvering zone (7) is 0-50% Q, 0-30% Q and 0-30% Q, respectively; the backflow amount of the sludge external backflow system is 50-100% Q.
3. A sewage treatment process characterized by performing sewage treatment by the fluidized bed-microaerobic multistage AO denitrification sewage treatment apparatus according to claim 1 or 2.
4. The wastewater treatment process according to claim 3, wherein the treatment process comprises the following steps:
closing the water inlet pipe orifices of the maneuvering area (7) and opening the other 3 water inlet pipe orifices; opening the first gate (10) and closing the second gate (11); the aeration I area (4), the aeration II area (6) and the maneuvering area (7) are adjusted into aerobic areas through an accurate aeration system (17); closing the mixed liquid internal reflux outlet of the aeration II area (6) and the mixed liquid internal reflux inlet of the maneuvering area (7), and opening the rest mixed liquid internal reflux inlets and outlets; opening a sludge external reflux system (16); then sewage is introduced and treated in each treatment area.
5. The wastewater treatment process according to claim 3, wherein the operation process is as follows:
opening the 4 water inlet pipe orifices, opening the first gate (10), and closing the second gate (11); the maneuvering zone (7) is adjusted to be an anoxic zone through an accurate aeration system (17), and the aeration zone I (4) and the aeration zone II (6) are adjusted to be an aerobic zone; opening all mixed liquid backflow inlets and outlets, and opening a sludge external backflow system (16); then sewage is introduced and treated in each treatment area.
6. The wastewater treatment process according to claim 3, wherein the operation process is as follows:
closing the water inlet pipe orifice of the maneuvering area (7) and opening other water inlet pipe orifices; closing the first gate (10) and opening the second gate (11); starting an aerator in the sludge regeneration zone (2) and carrying out controlled aeration; the inside of the aeration I area (4), the aeration II area (6) and the maneuvering area (7) are adjusted into a micro aerobic area through an accurate aeration system (17); an internal reflux outlet of the aeration II zone (6) and an internal reflux inlet of the maneuvering zone (7) are closed, and a sludge external reflux system (16) is opened; then sewage is introduced and treated in each treatment area.
7. The wastewater treatment process according to claim 3, wherein the operation process is as follows:
opening the four water inlet pipe orifices, closing the first gate (10) and opening the second gate (11); starting an aerator in the sludge regeneration zone (2) to carry out controlled aeration; adjusting an aeration I area (4) and an aeration II area (6) into a micro aerobic area through a precise aeration system (16); closing an aerator in the maneuvering zone (7), opening a flow pusher in the maneuvering zone (7), and adjusting the maneuvering zone (7) into an anoxic zone; opening all the mixed liquid internal reflux inlets and outlets, and opening a sludge external reflux system (16); then sewage is introduced and treated in each treatment area.
8. The wastewater treatment process according to claim 4, 5, 6 or 7, wherein the dissolved oxygen value of the anaerobic zone (1) of the fluidized bed is 0 to 0.2mg/L, the dissolved oxygen value of the anoxic zone is 0.2 to 0.5mg/L, and the dissolved oxygen value of the aerobic zone is 2mg/L or more.
9. The sewage treatment process according to claim 6 or 7, wherein the dissolved oxygen value of the microaerobic zone is 0.2 to 1.0mg/L, and the dissolved oxygen value of the sludge regeneration zone is 0.2 to 0.5 mg/L.
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